EP1245271A2 - Appareil et procédé pour préparer trialkoxysilanes practiquement exempts de chlore - Google Patents

Appareil et procédé pour préparer trialkoxysilanes practiquement exempts de chlore Download PDF

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Publication number
EP1245271A2
EP1245271A2 EP02003094A EP02003094A EP1245271A2 EP 1245271 A2 EP1245271 A2 EP 1245271A2 EP 02003094 A EP02003094 A EP 02003094A EP 02003094 A EP02003094 A EP 02003094A EP 1245271 A2 EP1245271 A2 EP 1245271A2
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Prior art keywords
silicon
copper
catalyst
reaction
inert solvent
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EP02003094A
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German (de)
English (en)
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EP1245271B1 (fr
EP1245271A3 (fr
Inventor
Frank Dr. Steding
Gerda Dr. Grund
Burkhard Dr. Standke
Frank Dr. Kropfgans
Michael Dr. Horn
Albert-Johannes Dr. Frings
Jaroslaw Dr. Monkiewicz
Hans-Günther Dr. Srebny
Claus-Dietrich Seiler
Hans-Joachim Dr. Kötzsch
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Evonik Operations GmbH
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Degussa GmbH
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
    • C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic Table
    • C07F7/02—Silicon compounds
    • C07F7/025—Silicon compounds without C-silicon linkages

Definitions

  • the invention relates to a method and an apparatus for producing trialkoxysilanes of the general formula I.
  • the base can be catalyzed dismutation of hydrogenalkoxysilanes
  • Monosilanes can be obtained in high purity. These can be found, for example, in Area of semiconductor industry use.
  • Hydrogen alkoxysilanes such as triethoxysilane (TEOS) or trimethoxysilane (TMOS) are on an industrial scale nowadays about esterification of trichlorosilane with Made ethanol or methanol.
  • Trichlorosilane is obtained in technical Order of magnitude by reacting elemental silicon with hydrogen chloride.
  • the Technically used processes for the production of TMOS and TEOS comprises two Process stages, trichlorosilane synthesis and the subsequent esterification. Both Due to the known high chemical aggressiveness, levels require Hydrogen chloride is a high investment in the plant and high consequential costs for the Maintenance of such a system.
  • trichlorosilane synthesis delivers a lot Effort to dispose of self-igniting residues containing chlorine. After this Processed TEOS or TMOS has a clear chlorine content. The chlorine content in these products is only very expensive Distillation process can be lowered into the ppm range.
  • Reaction temperature set using only about 8% of methanol used silicon to organosilanes by - about 5% to TMOS and about 3% to Tetramethoxysilane. Due to the lower reactivity of ethanol settle under otherwise identical reaction conditions only 6% of the silicon used to organosilanes by - approx. 5% TEOS and approx. 1% tetraethoxysilane. Propanol and Butanol are even less reactive chemically; silicon sales are 1.5% and 0.7%.
  • the invention is therefore based on the object of an economical method for To develop production of essentially chlorine-free trialkoxysilanes.
  • the object is achieved according to the information in the Claims resolved.
  • the present invention therefore relates to a process for the preparation of essentially halogen-free, preferably essentially chlorine-free trialkoxysilanes of the general formula I.
  • (RO) 3 SiH where R is an alkyl group having 1 to 6 carbon atoms, linear or branched alkyl groups are preferred, by reacting silicon with alcohols in an inert solvent in the presence of a copper-containing catalyst, which is characterized in that at least one organic copper compound is used as the catalyst.
  • the inventive method for the preparation of trialkoxysilanes general formula I is generally a process in which among the prevailing reaction conditions both gaseous, solid and liquid Components are involved.
  • a suitable solvent is a hydrocarbon-based one Heat transfer oil, preferably a tritoluol isomer mixture, especially preferably MARLOTHERM® S.
  • the inert solvent is used for The inventive method usually as a reaction medium, the used silicon can be suspended in it.
  • copper compounds are used as the catalyst used, which is preferably used in the inert solvent or in the Alcohol are soluble. Ethanol or methanol are preferably used as alcohol.
  • the catalyst is preferably in the reaction medium solved, d. H. is generally present in a homogeneously distributed form Benefits. Essentially chlorine-free copper compounds in one Reaction medium are soluble, could be a particularly cheap one Cause reaction behavior.
  • Copper alkylates are preferred as catalysts in the process according to the invention or copper alkoxylates or copper carboxylates.
  • Particularly preferred copper carboxylates containing 3 to 9 carbon atoms are used as catalysts, those with 7 to 9 carbon atoms are very particularly preferred.
  • neocarboxylic acids are used for the production of copper carboxylates used.
  • Copper carboxylates are made, for example, from copper hydroxide and / or copper oxide, which originate from an essentially chlorine-free production process, and one Carboxylic acid prepared with removal of the water of reaction.
  • Copper hydroxide and / or copper oxide preferably with a stoichiometric Amount of carboxylic acid, for example in a molar ratio of 1: 2, and Unreacted carboxylic acid can be distilled together with the water of reaction be removed.
  • the reaction can be carried out in a rotary evaporator be performed.
  • Removal of the water of reaction is preferred either by drag distillation or by vacuum distillation, suitably in the temperature range between 20 and 180 ° C, preferably in Temperature range between 140 and 180 ° C carried out.
  • the maximal Temperature is determined by the thermal stability of the copper alkoxylates or Limited copper carboxylates and should therefore usually be ⁇ 280 ° C.
  • the Use of nitrogen for inerting and lowering partial pressure is also possible.
  • Copper carboxylates can also be made of metallic copper and one Carboxylic acid are produced. Doing so with an excess of free Carboxylic acid to be worked. This implementation is preferably carried out at one Temperature between 140 and 180 ° C. But as a copper source, too Burns containing Si and Cu from the preparation of the trialkoxysilanes of the general Formula I can be used. After the reaction of the copper with the Carboxylic acid is generally filtered off insoluble components and that Filtrate, as already described above, freed from excess acid by distillation.
  • a powdery silicon largely freed from surface oxygen and silicon oxide, particularly preferably with a grain size d 90 of 20 to 1000 ⁇ m and d 50 of 10 to 800 ⁇ m, preferably d 50 of 20 to 500 ⁇ m, particularly preferably d 50 from 30 to 200 ⁇ m, very particularly preferably d 50 from 10 to 100 ⁇ m, are used.
  • the grain size distribution (d values) was determined by means of laser diffraction (device type: Microtrac - "full range analyzer", from Leeds and Northrup).
  • the silicon used here preferably contains less than 0.1% by weight of iron.
  • Process yields of more than 80%, based on the silicon used, possible the Fe content of the silicon used preferably being 0.03% by weight does not exceed.
  • the TEOS yield is around 50%, so far the Fe content of the silicon is in the range of 0.4% by weight.
  • Trialkoxysilanes of general formula I should work largely iron-free and the contact of the reaction mixture with iron can be avoided.
  • glass reactors, enamelled reactors, copper reactors, copper-plated reactors as well as tools and apparatus with comparable Texture and comparable surface properties for that inventive methods are used.
  • the silicon used for the implementation in the process according to the invention can by treatment with hydrogen fluoride, the solution used preferably 0.1 to 40% by weight HF, particularly preferably 0.5 to 5% by weight HF, contains.
  • the silicon used is treated suitably in an aqueous and / or alcoholic medium, preferably in a temperature between 0 and 100 ° C, preferably between 0 and 50 ° C, particularly preferably between 10 and 40 ° C and very particularly preferred between 20 and 30 ° C.
  • the silicon used for the reaction can also be in an aqueous and / or alcoholic medium pretreated with a pH> 10.
  • As basic medium is preferably sodium hydroxide solution, particularly preferably with a content of between 0.1 and 50% by weight of NaOH, very particularly preferably with a content between 0.1 and 10 wt .-% NaOH, used.
  • the silicon powder is suitably activated in a stirrer with inert gas overlay, e.g. B. nitrogen.
  • the treatment time to activate the Silicon is usually at least one minute, preferably 5 minutes to 1 hour, particularly preferably 15 to 30 minutes.
  • a silicon treatment time shouldn't be a quarter of an hour exceed.
  • Silicon treated in this way can be separated from the aqueous and / or alcoholic phase oxygen-poor conditions, for example by filtration, separated, with water, preferably oxygen-poor water, and / or alcohols, preferably methanol or ethanol, washed and then also under low oxygen Conditions are handled.
  • the residual fluorine levels are from silicon activated at around 50 ppm by weight up to the detection limit of fluorine.
  • the treated silicon can also be dried, preferably under vacuum, particularly preferably under vacuum at one Temperature between 0 and 180 ° C, for example in a rotary evaporator.
  • the drying of the activated silicon can also in other technical Drying equipment, e.g. B. a paddle dryer, preferably under inertized conditions.
  • the silicon powder After drying, the silicon powder is in the Generally operational.
  • the shelf life and handling of the extreme Oxygen sensitive powder can be improved and relieved if immediately after the treatment or after drying, the activated silicon, for example suspended in MARLOTHERM S®.
  • the suspension can be used directly for the Process according to the invention for the preparation of trialkoxysilanes of the general Formula I can be used.
  • the suspension is usually much less more sensitive to oxygen than the dry activated powder.
  • the use of such Suspension generally does not lead to any contact, even after about 1 hour of air contact significant loss of activity.
  • Activated silicon is still used until implementation to trialkoxysilanes of the general formula I, preferably under one low oxygen, inert liquid, particularly preferably below that for the Reaction used inert reaction medium, handled.
  • the reaction of silicon with alcohols in an inert solvent is used in The inventive method in the presence of an organic copper compound as Catalyst generally in the temperature range between 100 and 350 ° C, preferably in the temperature range between 180 and 260 ° C, particularly preferably in Temperature range between 200 and 250 ° C carried out.
  • reaction of silicon with alcohols in the invention Process in an inert solvent in the presence of an organic copper Compound as a catalyst, preferably at pressures from 1 to 5 bar abs., particularly preferably carried out at pressures between 1 and 3 bar abs.
  • the catalyst When carrying out the reaction of silicon with alcohols in an inert Solvent in the presence of an organic copper compound as a catalyst can in the process according to the invention, the catalyst also during the reaction be replenished.
  • the catalyst can, for example, in the Reaction used alcohol or in that used as the reaction medium inert solvents can be dissolved and replenished.
  • inventive implementation of silicon with alcohols in an inert Solvent in the presence of an organic copper compound as a catalyst suitably also in the presence of a defoamer, especially in Presence of a methyl silicone oil, which preferably has a viscosity between 0.65 up to 1,000,000 mPa s.
  • a defoamer especially in Presence of a methyl silicone oil, which preferably has a viscosity between 0.65 up to 1,000,000 mPa s.
  • Dimethylpolysiloxanes with a molecular weight between 162 and 74,000 g / mol or appropriate mixtures can be used as defoamers.
  • the inventive method for the preparation of trialkoxysilanes general formula I, the reaction of silicon with alcohols in an inert Solvent in the presence of an organic copper compound as a catalyst includes, can be carried out batchwise or continuously.
  • the present invention therefore also relates to a device for the continuous production of essentially halogen-free, preferably essentially chlorine-free trialkoxysilanes of the general formula I (RO) 3 SiH where R is an alkyl group having 1 to 6 carbon atoms, linear or branched alkyl groups are preferred, based on a main reactor unit (1), at least one dosing unit (2, 3, 4) upstream of the main reactor for liquids and / or suspensions and at least one dosing unit (5) for gaseous and / or vaporous substances as well as a unit (6 ) for product refurbishment.
  • R is an alkyl group having 1 to 6 carbon atoms, linear or branched alkyl groups are preferred, based on a main reactor unit (1), at least one dosing unit (2, 3, 4) upstream of the main reactor for liquids and / or suspensions and at least one dosing unit (5) for gaseous and / or vaporous substances as well as a unit (6 ) for product refurbishment.
  • FIG 1 is the schematic of a preferred embodiment of the device for the continuous production of essentially halogen-free, in particular chlorine-free, trialkoxysilanes represented by the general formula I.
  • the Main reactor unit (1) generally includes a heatable one Bubble column reactor (1.1), with multi-stage stirring device (1.1.1) and Jacket heating via the heat exchanger (1.9).
  • a return condenser (1.2) is suitably attached, it serves for the separation of the top product from the high boilers.
  • the high boilers for example the inert one Solvents usually run back into the container as a liquid phase in the 1.3 Bubble column reactor back.
  • the header product generally contains that Trialkoxysilane and excess alcohol and small amounts of the solvent.
  • the device (1.2) can have a further condensation device (1.4) and a Collection container for overhead product (1.5) must be connected downstream.
  • a bottom product container (1.6) from which the further processing of the bottom product takes place, preferably the Separation of the discharged silicon from the solvent.
  • the Bottom product container (1.6) is usually equipped with a stirring device (1.6.1). This can be done using a circulation pump (1.7) and a heat exchanger (1.8) Bottom product can be circulated via the container (1.6).
  • the bottom product contains generally only solvent in the liquid phase and not as a solid implemented silicon.
  • the dosing units (2), (3), (4) and (5) can be used to carry out the Process according to the invention necessary educts the bubble column reactor be fed.
  • the metering unit (2) suitably also contains a storage container (2.1) Feed (2.3), a stirring device (2.1.1), an inert gas (2.5), a circulation pump (2.2) and the possibility of using a heat exchanger (2.4) Preheat the feed stream.
  • the dosing unit (2) is preferred for dosing and Feeding the catalyst solution into the main reactor unit (1).
  • the dosing unit (4) preferably also contains a storage container (4.1) Feed (4.2), a circulation pump (4.2) and the possibility of using a Heat exchanger (4.3) to preheat the educt flow.
  • the dosing unit (4) is preferably for metering and feeding the solvent into the Main reactor unit (1) used.
  • the dosing unit (3) preferably contains a storage container for solids (3.1) with a suitable feed (3.2), e.g. B. via pneumatic conveying, a Inert gas (3.3) and a filter device (3.4) for Solids separation.
  • the dosing unit (3) is preferred for dosing and Feed of silicon powder used in the main reactor unit (1).
  • the dosing unit (5) preferably contains devices for dosing Gases (5.5), for example for nitrogen and gaseous starting materials or one Device for storing (5.1) and subsequently metering a liquid, such as methanol or ethanol, which, for example, can also be evaporated (5.3), preferably in the form of a heat exchanger, in the gas or vapor phase can be transferred.
  • the dosing unit (5) is preferred for dosing and Feeding alcohols used in the main reactor unit (1).
  • the main reactor unit (1) is suitably a product workup (6) downstream.
  • This generally consists of thermal separation processes Separation of components, e.g. B. a distillation column (6.1) for separation the unreacted alcohol from the trialkoxysilane and the distillation column (6.2) for the separation of higher-boiling components, essentially the Solvent.
  • Working up via distillation columns is preferred with low hold-up.
  • the use and combination of Thin film evaporators, falling film evaporators and distillation columns for Gentle processing with short dwell times is also possible.
  • Unreacted alcohol for example from product workup (6), can be fed back into the process via the dosing unit (5).
  • online hydrogen analysis is preferred in the method according to the invention (1.10), e.g. using an on-line thermal conductivity detector (WLD) used.
  • WLD thermal conductivity detector
  • This is preferred to the vapor line of the Bubble column reactor connected, particularly preferably before the condenser (1.4).
  • the bottom product preferably enters a bottom product from the bottom product container (1.6) Working up for the separation of solids, particularly preferably a filter centrifuge or Decanter.
  • the unreacted silicon is removed via the discharge device (7.2) carried out and can be further processed.
  • the Solvents and higher-boiling, liquid components are used in the Discharge device (7.3) carried out and can partially over the Dosing device (4) can be recirculated.
  • Unreacted alcohol for example from product workup (6), can be fed back into the process via the dosing unit (5).
  • Organic copper compounds are generally among those mentioned above Reaction conditions are only stable to a limited extent over a longer period of time. Nevertheless cause the organic copper used in the inventive method Excellent catalytic activity, very good selectivity and high yields.
  • such copper catalysts have the advantage of declining catalyst activity in liquid form, d. H. as a homogeneous solution to be able to be metered into the reaction mixture in a simple manner.
  • inventive method in a continuously operated process be carried out particularly economically.
  • Trialkoxysilanes of the general formula I prepared as a rule have only chloride levels ⁇ 3 ppm by weight.
  • Batch trialkoxysilane synthesis under normal pressure The laboratory equipment described below was used: Heated 500 ml glass stirred reactor, equipped with nitrogen blanket, temperature measuring device, alcohol and catalyst metering device via immersion tube by means of a metering pump, distillation device, consisting of 20 cm glass column (filling: ceramic saddle body), Dimroth cooler and distillation receiver.
  • the reactor is blanketed with nitrogen 30 g activated silicon, suspended in 250 g MARLOTHERM® S, and if appropriate, charged solid catalyst and heated to about 200 to 250 ° C.
  • the catalyst is then initially used in a period of 0.5 to 4 hours (approx. 1 g Cu carboxylate in 30 g alcohol) fed via the metering pump, then the Alcohol (dosage: approx. 5 ml / min).
  • Catalyst (1 g Cu carboxylate in 30 g alcohol) at approx. 1 hour intervals be replenished.
  • the hydrogen developed is used as a measure of silicon sales determined volumetrically via a laboratory gas meter. In regular Intervals (approx.
  • the duration of the reaction is between 4 and 6 hours.
  • the achievable sales are between 82 to 90% silicon, which achieve selectivities to trialkoxysilane 95 to 97%.
  • the catalyst requirement is with an average of 3.5% Cu Weight of silicon low.
  • the space-time yields in the discontinuous experiments are approx. 1 mol / l h trialkoxysilane.
  • Example 2 Discontinuous trialkoxysilane synthesis under increased pressure: The glass apparatus described in Example 1 is replaced by a functionally equivalent, pressure-resistant apparatus. Enameled steel, copper or steel reactors with a copper inner jacket are considered as materials for the reactor.
  • the reaction corresponds to the operating mode under normal pressure. Behind the Distillate template, a pressure control is installed, the desired system pressure holds.
  • Preparation of the catalyst is carried out in a 1 liter glass rotary evaporator.
  • the apparatus can be evacuated via a connected water jet vacuum pump. Inertisation is also possible with nitrogen.
  • the apparatus is rendered inert with nitrogen and slowly cooled to about 70 to 80 ° C. At this temperature, approx. 600 g of ethanol are placed in the flask of the Rotated evaporator and mixed with the reaction product.
  • the apparatus is then cooled further. At about 30 to 40 ° C Product removed.
  • the catalyst thus produced is ready for use.
  • CuCl 2 can be added to the catalyst described according to the invention; in the Cu: Cl molar ratio of 10: 1, this corresponds to an addition of 0.041 mol of CuCl 2 for the above reaction mixture.
  • Discontinuous production of triethoxysilane with HF activated, stored silicon The reaction is carried out in a 2 liter glass reactor with stirrer, attached distillation column, filled with glass-Raschig rings, and a downstream cooler and distillate receiver.
  • the alcohol is dosed via a dip tube through a dosing pump.
  • the catalyst solution is either carried out via an additional metering pump and a further immersion tube or manually via an injection.
  • the distillate is collected in fractions.
  • a gas meter is installed in the exhaust gas from the distillate receiver as a volume gas meter.
  • the reactor is time programmed to approx. 240 to 250 ° C.
  • the alcohol introduced over the silicon powder distills off.
  • gas, H 2 there is a significant evolution of gas, H 2 .
  • the gas volume flow can be determined directly on the volumetric gas meter, which is connected downstream of the distillate feed. The course of the reaction can be followed via the gas volume flow.
  • ethanol is dosed. Through the When the exothermic reaction begins, the temperature quickly rises to 250 ° C.
  • the Ethanol dosage is between 10 to 20 g / minute.
  • the distillate is collected in fractions and weighed.
  • the Product composition is determined using gas chromatography.
  • the total reaction time is between 4 and 6 hours.
  • the achievable Sales are between 82 to 90% of the silicon introduced, the selectivities to triethoxysilane are 95 to 97%.
  • the catalyst requirement is with 3.5% copper, based on the amount of silicon used, low.
  • the space-time yield for Triethoxysilane is on average about 1.4 mol / h l.
  • test results for Example 5 are listed in Table 1 and shown graphically in FIG. 2.
  • the test facility for the continuous production of trialkoxysilanes of the general formula I essentially comprises the device described in more detail on pages 9 and following.
  • the silicon is activated according to Example 3 in a functional manner equivalent pilot plant equipment with a reactor volume of approx. 250 I. approx. 50 kg silicon, 90 kg 1% are at the same proportions of the starting materials Hydrofluoric acid and 71 kg of ethanol.
  • the catalyst according to Example 4 is produced in a functionally equivalent pilot plant with a reactor volume of approx. 35 I. Approx. 6.8 kg of neononanoic acid, 1.8 kg of Cu (OH) 2 and 13.4 are obtained with the same proportions of the starting materials kg of ethanol used.
  • the reaction is carried out in a 10 l steel bubble column with a copper jacket and copper internals carried out.
  • the bubble column equipped with a multi-stage stirrer an inner diameter of about 0.2 m and is with an attached column and Provide partial return condenser.
  • the vapors are condensed and then sent for rectification. Alcohol is evaporated and over you Gas distributor at the bottom of the bubble column.
  • the gas distributor is an annular nozzle designed with downward bores.
  • activated silicon (d V50 approx. 15 ⁇ m) and solvent as approx. 20% suspension are fed into the reactor as a starting batch. Catalyst, about 4% copper with respect to the amount of silicon, is added. Analogous to the discontinuous operation, the reactor is time-programmed to about 200 ° C., then the metering of alcohol, about 120 mol / h, was started. This is evaporated in a preheater and inserted via a gas distributor at the bottom of the bubble column. The temperature is increased to 250 ° C. at normal pressure. The course of the reaction is continuously monitored in the exhaust gas stream by means of the H 2 development by means of an "on-line thermal conductivity detector (TCD)".
  • TCD on-line thermal conductivity detector
  • the reaction can be carried out with approx. 4 kg / h ethanol and a molar dosing ratio of 6.5 mol of ethanol, based on 1 mol of silicon become.
  • the silicon solids content can vary between 15 and 30%, 20% solids content is preferred.
  • the catalyst dosage is 3 up to 4 g of copper, based on 100 g of silicon. Be over the condensed distillate 7.5 mol / h triethoxysilane obtained.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
EP02003094A 2001-03-30 2002-02-13 Appareil et procédé pour préparer trialkoxysilanes practiquement exempts de chlore Expired - Lifetime EP1245271B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10116007 2001-03-30
DE10116007A DE10116007A1 (de) 2001-03-30 2001-03-30 Vorrichtung und Verfahren zur Herstellung von im Wesentlichen halogenfreien Trialkoxysilanen

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EP1245271A2 true EP1245271A2 (fr) 2002-10-02
EP1245271A3 EP1245271A3 (fr) 2003-09-17
EP1245271B1 EP1245271B1 (fr) 2007-11-21

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EP (1) EP1245271B1 (fr)
JP (1) JP2002326994A (fr)
DE (2) DE10116007A1 (fr)

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US7652164B2 (en) 2005-09-13 2010-01-26 Momentive Performance Materials Inc. Process for the direct synthesis of trialkoxysilane
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DE102007050573A1 (de) * 2007-10-23 2009-04-30 Evonik Degussa Gmbh Großgebinde zur Handhabung und für den Transport von hochreinen und ultra hochreinen Chemikalien
DE102007059170A1 (de) * 2007-12-06 2009-06-10 Evonik Degussa Gmbh Katalysator und Verfahren zur Dismutierung von Wasserstoff enthaltenden Halogensilanen
DE102008004396A1 (de) * 2008-01-14 2009-07-16 Evonik Degussa Gmbh Anlage und Verfahren zur Verminderung des Gehaltes von Elementen, wie Bor, in Halogensilanen
DE102008002537A1 (de) * 2008-06-19 2009-12-24 Evonik Degussa Gmbh Verfahren zur Entfernung von Bor enthaltenden Verunreinigungen aus Halogensilanen sowie Anlage zur Durchführung des Verfahrens
DE102011006053A1 (de) 2011-03-24 2012-09-27 Evonik Degussa Gmbh Verfahren zur Dechlorierung von alkylfunktionellen Organosilanen und alkylfunktionellen Organosiloxanen
RU2744612C2 (ru) 2016-03-16 2021-03-11 Констракшн Рисерч Энд Текнолоджи Гмбх Ингибитор коррозии, наносимый на поверхность
CN110357915B (zh) * 2018-04-11 2023-02-03 台湾特品化学股份有限公司 硅乙烷合成及过滤纯化的系统
DE102018210886A1 (de) 2018-07-03 2020-01-09 Evonik Degussa Gmbh Verfahren zur Herstellung von Alkylalkoxysilanen
RU2752507C1 (ru) * 2020-09-14 2021-07-28 Федеральное государственное бюджетное учреждение науки Институт элементоорганических соединений им. А.Н. Несмеянова Российской академии наук (ИНЭОС РАН) Реактор для получения алкоксисиланов
RU2762563C1 (ru) * 2020-12-30 2021-12-21 Федеральное государственное бюджетное учреждение науки Институт элементоорганических соединений им. А.Н. Несмеянова Российской академии наук (ИНЭОС РАН) Реактор для механохимического синтеза алкоксисиланов

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EP1245271B1 (fr) 2007-11-21
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US6727375B2 (en) 2004-04-27
DE50211242D1 (de) 2008-01-03
EP1245271A3 (fr) 2003-09-17
DE10116007A1 (de) 2002-10-02

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